Classifications

• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
  • C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
  • C08F210/04—Monomers containing three or four carbon atoms
  • C08F210/06—Propene
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
  • C08J5/00—Manufacture of articles or shaped materials containing macromolecular substances
  • C08J5/18—Manufacture of films or sheets
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
  • C08J2323/00—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers
  • C08J2323/02—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers not modified by chemical after treatment
  • C08J2323/10—Homopolymers or copolymers of propene
  • C08J2323/14—Copolymers of propene
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
  • C08L23/00—Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Compositions of derivatives of such polymers
  • C08L23/02—Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Compositions of derivatives of such polymers not modified by chemical after-treatment
  • C08L23/10—Homopolymers or copolymers of propene
  • C08L23/14—Copolymers of propene

Definitions

• the present invention relates to a multimodal copolymers of propylene and 1-hexene having a content of 1-hexene derived units ranging from 0.6 wt to 3.0 wt especially suitable for the production of industrial sheets.
• Copolymers of propylene and hexene-1 having a low 1-hexene content are known in the art.
• WO 2006/002778 relates to a random polymer of propylene and 1-hexene contains from 0.2 to 5 wt , recurring units derived from hexene-1.
• the propylene -hexene- 1 polymer exhibits broad molecular weight distribution of monomodal type.
• WO 2009/083500 relates to plastic tanks made from propylene copolymers of
• exemplified has a distribution of the monomodal type.
• an object of the present invention is a propylene- 1-hexene copolymer having a multimodal distribution of molecular weight having improved mechanical properties in particular improved flexural modulus.
• An object of the present invention is a propylene-hexene-1 copolymers having;
• a content of 1-hexene derived units ranging from 0.6 wt to 3.0 wt ; preferably from 0.7 wt to 2,0 wt ; more preferably from 0.8 wt to 1.5 wt ;
• melt flow rate measured according to the method ISO 1133 (230° C, 5 kg) ranging from 0.5 g/10 min to 5.0 g/10 min preferably from 0.6 g/10 min to 4.0 g/10 min; more preferably from 0.7 g/10 min to 2.0 g/10 min;
• the polydispersity (PI) ranges from 4.5 to 10; preferably from 4.5 to 6;
• the melting point ranges from 160°C to 145°C ; preferably from 155°C to 147°C; more preferably from 153°C to 150°C;
• Figure 1 is the DSC thermogram of the propylene- 1-hexene copolymer of example 1;.
• Figure 2 is the DSC thermogram of the propylene- 1-hexene copolymer of comparative example 2.
• molecular weight distribution of multimodal type is meant therein that there are at least two peaks in the DSC curve (temperature/heat of fusion).
• a peak is defined as a point on the DSC curve (temperature/heat of fusion) having the highest value of heat of fusion at a temperature A with respect to the values of heat of fusion in the range + 1 °C with respect to temperature A.
• the propylene-hexene-1 copolymer object of the present invention in endowed with improved value of flexural modulus with respect to a copolymer having a monomodal distribution.
• the flexural modulus is higher than 1350 MPa and the IZOD is higher than 26 Kj/m 2 ; preferably higher than 28 Kj/m 2.
• An industrial sheet is defined as a sheet having a thickens higher than 0.1 mm; preferably higher than 0.3 mm.
• a further object of the present invention is an industrial sheet comprising the propylene- 1-hexene of the present invention.
• the propylene-hexene-1 polymers of the present invention can be prepared by
• inventions comprise a solid catalyst component comprising at least one titanium compound having at least one titanium-halogen bond and at least an electron-donor compound (internal donor), both supported on magnesium chloride.
• the Ziegler-Natta catalysts systems further comprise an organo-aluminum compound as essential co-catalyst and optionally an external electron-donor compound.
• the solid catalyst component comprises Mg, Ti, halogen and an electron donor selected from esters of phthalic acids disclosed in EP45977 and in particular of either diisobutylphathalate or dihexylphthalate or diethylphthalate and mixtures thereof.
• the solid catalyst component can be prepared by reacting a titanium compound of formula Ti(OR) n - y X y , where n is the valence of titanium and y is a number between 1 and n, preferably TiCl 4 , with a magnesium chloride deriving from an adduct of formula MgCl 2 pROH, where p is a number between 0.1 and 6, preferably from 2 to 3.5, and R is a hydrocarbon radical having 1-18 carbon atoms.
• the adduct can be suitably prepared in spherical form by mixing alcohol and magnesium chloride in the presence of an inert hydrocarbon immiscible with the adduct, operating under stirring conditions at the melting temperature of the adduct (100-130 °C). Then, the emulsion is quickly quenched, thereby causing the solidification of the adduct in form of spherical particles. Examples of spherical adducts prepared according to this procedure are described in US 4,399,054 and US 4,469,648.
• the so obtained adduct can be directly reacted with the Ti compound or it can be previously subjected to thermal controlled dealcoholation (80-130 °C) so as to obtain an adduct in which the number of moles of alcohol is generally lower than 3, preferably between 0.1 and 2.5.
• the reaction with the Ti compound can be carried out by suspending the adduct (dealcoholated or as such) in cold TiCl 4 (generally 0 °C); the mixture is heated up to 80-130 °C and kept at this temperature for 0.5-2 hours.
• the treatment with TiCl 4 can be carried out one or more times.
• the internal donor can be added during the treatment with TiCl 4 and the treatment with the electron donor compound can be repeated one or more times.
• the internal donor is used in molar ratio with respect to the MgCl 2 of from 0.01 to 1 preferably from 0.05 to 0.5.
• the preparation of catalyst components in spherical form is described for example in European patent application EP- A-395083 and in the International patent application WO98/44001.
• the solid catalyst components obtained according to the above method contain the titanium compound, expressed as Ti, generally in an amount from 0.5 to 10% by weight. [0023] Moreover, they show a surface area (by B.E.T. method) generally between 20 and
• the porosity (Hg method) due to pores with radius up to 10.000A generally ranges from 0.3 to 1.5 cm /g, preferably from 0.45 to 1 cm 3 /g.
• the organo-aluminum compound is preferably an alkyl-Al selected from the trialkyl aluminum compounds such as for example triethylaluminum, triisobutylaluminum, tri-n- butylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum. It is also possible to use mixtures of trialkylaluminum's with alkylaluminum halides, alkylaluminum hydrides or alkylaluminum sesquichlorides such as AlEt 2 Cl and Al 2 Et 3 Cl 3 .
• the Al-alkyl compound is generally used in such a quantity that the Al/Ti ratio be from 1 to 1000.
• Preferred external electron-donor compounds include silicon compounds, ethers, esters such as ethyl 4-ethoxybenzoate, amines, heterocyclic compounds and particularly 2,2,6,6-tetramethyl piperidine, ketones and the 1,3-diethers.
• Another class of preferred external donor compounds is that of silicon compounds of formula R a 5 R b 6 Si(OR 7 ) c , where a and b are integer from 0 to 2, c is an integer from 1 to 3 and the sum (a+b+c) is 4;
• R 5 , R 6 , and R are alkyl, cycloalkyl or aryl radicals with 1-18 carbon atoms optionally containing heteroatoms. Particularly preferred are methylcyclohexyldimethoxysilane,
• the external electron donor compound is used in such an amount to give a molar ratio between the organo- aluminum compound and said electron donor compound of from 0.1 to 500.
• polymer of te present invention is a solid catalyst component comprising a magnesium halide, a titanium compound having at least a Ti-halogen bond as above described and at least two electron donor compounds selected from succinates and the other being selected from 1,3 diethers, [0028]
• the catalysts generally used in the process of the invention are capable of producing polypropylene with a value of xylene insolubility at ambient temperature greater than
• the propylene-hexene-1 polymers of the present invention are produced by a
• the condition of fast fluidization in the riser is established by feeding a gas mixture comprising the relevant monomers to said riser. It is preferable that the feeding of the gas mixture is effected below the point of reintroduction of the polymer into said riser by the use, where appropriate, of gas distributor means.
• the velocity of transport gas into the riser is higher than the transport velocity under the operating conditions, preferably from 2 to 15 m/s.
• the polymer and the gaseous mixture leaving the riser are conveyed to a solid/gas separation zone.
• the solid/gas separation can be effected by using conventional separation means.
• the polymer enters the downcomer.
• the gaseous mixture leaving the separation zone is compressed, cooled and transferred, if appropriate with the addition of make-up monomers and/or molecular weight regulators, to the riser.
• the transfer can be carried out by means of a recycle line for the gaseous mixture.
• control of the polymer circulation between the two polymerisation zones can be carried out by metering the amount of polymer leaving the downcomer using means suitable for controlling the flow of solids, such as mechanical valves.
• the operating parameters are those that are usual in olefin polymerisation process, for example between 50 to 120 °C.
• the operating pressures can range between 0.5 and 10 MPa, preferably between 1.5 to 6 MPa.
• one or more inert gases such as nitrogen or an aliphatic hydrocarbon, are maintained in the polymerization zones, in such quantities that the sum of the partial pressures of the inert gases is preferably between 5 and 80% of the total pressure of the gases.
• the various catalysts are fed up to the riser at any point of the said riser. However, they can also be fed at any point of the downcomer.
• the catalyst can be in any physical state, therefore catalysts in either solid or liquid state can be used.
• the propylene-hexene-1 copolymers of the invention may also be blended with any other additives commonly employed in the art, such as antioxidants, light stabilizers, heat stabilizers, phenolic antioxidants, slip agents such as calcium stearate and any other nucleating agents selected among talc, aromatic carboxylic salts, salts of monocarboxylic or polycarboxylic acids, e.g. sodium benzoate, aluminum tert-butylbenzoate or dicetyl peroxydicarbonate.
• any other additives commonly employed in the art such as antioxidants, light stabilizers, heat stabilizers, phenolic antioxidants, slip agents such as calcium stearate and any other nucleating agents selected among talc, aromatic carboxylic salts, salts of monocarboxylic or polycarboxylic acids, e.g. sodium benzoate, aluminum tert-butylbenzoate or dicetyl peroxydicarbonate.
• IZOD Impact Strength determined according to ISO 180/1 A.
• Flexural modulus determined according to ISO 178.
• Propylene-hexene- 1 polymers are prepared by polymerising propylene and hexene-1 by polymerising propylene and hexene-1 in the presence of a catalyst under continuous conditions in a plant comprising a polymerisation apparatus as described in EP 1 012 195.
• examples 1 the gas composition in the two reactor legs has been differentiated by using the "barrier" feed according to what described in EP 1 012 195. This stream is propylene fed in the larger upper part of the downcomer. In comparative example 2 the barrier feed has not been used.
• the catalyst employed comprises a catalyst component prepared by analogy with example 5 of EP-A-728769 but using microspheroidal MgCl 2 - I.7C 2 H 5 OH instead of MgCl 2 -2.1C 2 H 5 0H.
• Such catalyst component is mixed with dicyclopentyl dimethoxy silane (DCPMS) as external donor and with triethylaluminium (TEAL) in the precontact section.
• DCPMS dicyclopentyl dimethoxy silane
• TEAL triethylaluminium
• the catalyst system is then subjected to pre-polymerisation before introducing it into the polymerisation apparatus.
• the polymer particles exiting the reactor are subjected to a steam treatment to remove the reactive monomers and volatile substances and then dried.
• the polymer particles are extruded with a usual packing of stabilisers.

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• 2014
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